US20120103186A1 - Method For Adjusting The Purity Of Oxygen Generated By An Adsorption Unit By Controlling The Flow Rate - Google Patents
Method For Adjusting The Purity Of Oxygen Generated By An Adsorption Unit By Controlling The Flow Rate Download PDFInfo
- Publication number
- US20120103186A1 US20120103186A1 US13/378,062 US201013378062A US2012103186A1 US 20120103186 A1 US20120103186 A1 US 20120103186A1 US 201013378062 A US201013378062 A US 201013378062A US 2012103186 A1 US2012103186 A1 US 2012103186A1
- Authority
- US
- United States
- Prior art keywords
- oxygen
- purity
- flow rate
- vps
- production flow
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
- B01D53/0476—Vacuum pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0454—Controlling adsorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
- C01B13/0229—Purification or separation processes
- C01B13/0248—Physical processing only
- C01B13/0259—Physical processing only by adsorption on solids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/12—Oxygen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/102—Nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40007—Controlling pressure or temperature swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40007—Controlling pressure or temperature swing adsorption
- B01D2259/40009—Controlling pressure or temperature swing adsorption using sensors or gas analysers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/45—Gas separation or purification devices adapted for specific applications
- B01D2259/4525—Gas separation or purification devices adapted for specific applications for storage and dispensing systems
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0043—Impurity removed
- C01B2210/0046—Nitrogen
Definitions
- the present invention relates to a method for regulating a method or a unit for gas separation by adsorption, in particular a method or unit of the VSA type, producing an oxygen-rich gas from ambient air.
- the difficulty of controlling this oxygen purity resides in the selection of the action variables, given that there are many possibilities for controlling this purity: acting on the cycle times, the pressures in the adsorbers, the flow rates and/or pressures of the unit, etc.
- VSA methods for producing oxygen are currently controlled by simple control loops for pressure or flow rate at the compression output and/or maximum pressure in the adsorbers.
- the problem which then arises is to be able to minimize the provision of liquid oxygen by carrying out effective control of the VSA method and/or unit so as to improve its productivity.
- a solution of the invention is a method for producing gaseous oxygen from compressed air by adsorption, in which:
- VPS Pp+ X with X ⁇ 0.5%.
- X being the standard deviation
- the method according to the invention may have one or more of the following characteristics:
- the solution of the invention is therefore based on installing a loop for regulating the purity to a purity threshold value (VPS) on the O 2 VSA unit, the loop being intended to adjust the flow rate of oxygen produced (Dp) in real time so as to reduce the required quantity of liquid oxygen, referred to as “LOX”.
- VPS purity threshold value
- a flow rate limit of the VSA unit is set so that O 2 purity (Pp) in the oxygen-enriched gas produced by the VSA unit is always greater than the set threshold value (VPS) set by the client, for example at a purity of 90% by volume.
- This phenomenon is due in particular to climatic variations, such as day/night and summer/winter temperature differences, as can be seen in FIG. 1 .
- the principle of the control loop of the invention consists in adjusting this flow rate (Dp) in real time in order to ensure a purity of oxygen produced (Pp) equal to VPS or differing very little from VPS (standard deviation 0.1%) and therefore to avoid or minimize the use of LOX.
- This type of regulation therefore makes it possible to economize on LOX by optimizing the productivity of the VSA, to obtain a reduction in the number of procedures of the “purity search” type by adapting the flow rate of the VSA to the decrease in flow rate so as not to “lose” the O 2 purity, and leads to a reduction in the user interventions for modifying the regulation of the oxygen production flow rate (Dp).
- FIG. 2 schematizes the operating principle of a method according to the invention, applied to an adsorption unit 1 of the O2 VSA type producing oxygen whose purity has to be kept permanently at least at 90% by volume, which constitutes the desired purity threshold value (VPS).
- VPS desired purity threshold value
- the oxygen produced is recovered at the output of the O2 VSA (zone 1 ) and conveyed to a container (not shown) as far as a client site (zone 4 ) by means of at least one compressor (zone 2 ) by means of a pipeline.
- the recirculation valve Qr is driven according to a flow rate control loop or “loop FIC 1 ”.
- the function of the latter is to limit the production flow rate (Dp) of the unit to the value set by the operator, irrespective of the client demand (Du).
- the regulation principle of the invention therefore consists in adapting the reference of the loop FIC 1 as a function of the oxygen purity measurement (Pp).
- the principle of the control loop consists in adapting the production flow rate limit (Dp) in real time in order to ensure a purity at the capacity limits of the VSA unit.
- Dp production flow rate limit
- This adaptation is obtained by virtue of the functional diagram given in FIG. 3 and employing a so-called “predictive” or “Smith predictor” regulation algorithm.
- This injection of backup LOX is particularly advantageous because it makes it possible to cater for peaks in oxygen demand from the user site.
Abstract
The invention relates to a method for producing gaseous oxygen by adsorption from compressed air, comprising: a) using at least one adsorption unit for generating gaseous oxygen having a purity greater than or equal to a predetermined purity threshold value (VPS) and according to a variable production flow rate (Dp); b) recovering the gaseous oxygen produced in a); c) measuring the purity of the gaseous oxygen (Pp) produced in step a) and comparing same with a preset purity threshold value (VPS); and d) adjusting the oxygen production flow rate (Dp) on the basis of the comparison of step c) such that: i) reducing the oxygen production flow rate (Dp) when the oxygen purity (Pp) measured in step c) is such that VPS>Pp; or ii) increasing the production flow rate (Dp) when the oxygen purity determined in step c) is such that VPS<Pp in order to obtain a gaseous oxygen purity (Pp) such that VPS=Pp+X, with X<0.5%, X being the standard deviation.
Description
- The present invention relates to a method for regulating a method or a unit for gas separation by adsorption, in particular a method or unit of the VSA type, producing an oxygen-rich gas from ambient air.
- The possibility of controlling the purity of the oxygen-rich gas produced at the output of a unit for gas separation by adsorption, in particular a unit of the VSA type, has already been studied, particularly in documents U.S. Pat. No. 5,258,056.
- The difficulty of controlling this oxygen purity resides in the selection of the action variables, given that there are many possibilities for controlling this purity: acting on the cycle times, the pressures in the adsorbers, the flow rates and/or pressures of the unit, etc.
- In view of these difficulties, VSA methods for producing oxygen, commonly referred to as “O2 VSA methods”, are currently controlled by simple control loops for pressure or flow rate at the compression output and/or maximum pressure in the adsorbers.
- This absence of precise control often leads to a loss of productivity, which makes it necessary to provide an additional supply of liquid oxygen (LOX) for the user, when the production of the O2 VSA is insufficient to guarantee this user a minimum purity and/or oxygen flow rate for its application, for example to manufacture glass, paper pulp, to supply aquaculture or the like. This additional supply of liquid oxygen for the user in turn generates a significant extra cost.
- Document U.S. Pat. No. 5,258,056 teaches a PSA method for producing nitrogen from atmospheric air, in which the oxygen is an impurity to be eliminated. The level of impurities, i.e. oxygen, is used to control the supply of air entering the PSA system.
- Document U.S. Pat. No. 4,725,293 moreover describes a similar PSA method also making it possible to produce nitrogen from ambient air.
- The problem which then arises is to be able to minimize the provision of liquid oxygen by carrying out effective control of the VSA method and/or unit so as to improve its productivity.
- A solution of the invention is a method for producing gaseous oxygen from compressed air by adsorption, in which:
-
- a) gaseous oxygen having a purity greater than or equal to a given purity threshold value (VPS) is produced with a variable production flow rate (Dp) by means of at least one adsorption unit,
- b) the gaseous oxygen produced in a) is recovered and is conveyed by means of at least one gas pipeline to a user site or storage site,
- c) the purity of gaseous oxygen (Pp) produced in step b) and carried by said gas pipeline is measured before the user site or storage site and compared with the preset purity threshold value (VPS), and
- d) the oxygen production flow rate (Dp) is adjusted before the user site or storage site as a function of the comparison carried out in step c) so that:
- i) the oxygen production flow rate (Dp) is reduced when the oxygen purity (Pp) measured in step c) is such that: VPS>Pp or
- ii) the production flow rate (Dp) is increased when the oxygen purity (Pp) determined in step c) is such that: VPS<Pp so as to obtain a gaseous oxygen purity (Pp) such that:
-
VPS=Pp+X with X<0.5%. X being the standard deviation, -
- e) the produced oxygen is sent at a production flow rate (Dp) to a user site, and
- f) when the user flow rate (Du) is such that Du>Dp, oxygen coming from a source of liquid oxygen (LOX) is added to the gas pipeline, the liquid oxygen being vaporized before its introduction into the gas pipeline, so as to obtain a given user oxygen purity (Pu) such that: VPS=Pu+X
- where:
- the oxygen purity (Pu) is measured on the pipeline downstream of the injection site of liquid oxygen (LOX)
- the user flow rate (Du) is the flow rate of oxygen consumed by the user site.
- Depending on the case, the method according to the invention may have one or more of the following characteristics:
-
- the oxygen production flow rate is adjusted in step d) so that VPS=Pp+X with X<0.3%, preferably X<0.2%, more preferably X<0.1%;
- the recovered gaseous oxygen is compressed in step b) before it is conveyed to the user site by means of the gas pipeline;
- the gaseous oxygen is produced in step a) by an adsorption unit of the VSA or PSA type;
- the purity threshold value (VPS) is at least 70% by volume, preferably between 85 and 95%, advantageously from 90% to 93%;
- the oxygen is produced in step a) by separation of air by adsorption of nitrogen on at least one adsorbent which adsorbs nitrogen preferentially to oxygen, the adsorbent preferably being a zeolite;
- the oxygen production flow rate is adjusted in step d) by acting on the opening of a recirculation valve situated on a bypass line formed on the gas pipeline carrying the produced oxygen, said bypass line making it possible to bypass at least one gas compressor situated on said gas pipeline, downstream of the adsorption unit, and furthermore serving to recycle, upstream of said at least one compressor, oxygen collected downstream of said compressor;
- the production flow rate (Dp) is between 100 and 6000 Nm3/h;
- the user flow rate (Du) is between 100 and 10 000 Nm3/h;
- the purity (Pp) of the oxygen is between 88 and 95%; and
- the user oxygen purity (Pu) is between 88 and 100%.
- The solution of the invention is therefore based on installing a loop for regulating the purity to a purity threshold value (VPS) on the O2 VSA unit, the loop being intended to adjust the flow rate of oxygen produced (Dp) in real time so as to reduce the required quantity of liquid oxygen, referred to as “LOX”.
- Specifically, according to the current operating mode, a flow rate limit of the VSA unit is set so that O2 purity (Pp) in the oxygen-enriched gas produced by the VSA unit is always greater than the set threshold value (VPS) set by the client, for example at a purity of 90% by volume.
- However, this leads to O2 purity values (Pp) very much greater than the desired purity threshold value (VPS), which may reach for example 92% in certain cases.
- This phenomenon is due in particular to climatic variations, such as day/night and summer/winter temperature differences, as can be seen in
FIG. 1 . - The principle of the control loop of the invention consists in adjusting this flow rate (Dp) in real time in order to ensure a purity of oxygen produced (Pp) equal to VPS or differing very little from VPS (standard deviation 0.1%) and therefore to avoid or minimize the use of LOX.
- This type of regulation therefore makes it possible to economize on LOX by optimizing the productivity of the VSA, to obtain a reduction in the number of procedures of the “purity search” type by adapting the flow rate of the VSA to the decrease in flow rate so as not to “lose” the O2 purity, and leads to a reduction in the user interventions for modifying the regulation of the oxygen production flow rate (Dp).
-
FIG. 2 schematizes the operating principle of a method according to the invention, applied to anadsorption unit 1 of the O2 VSA type producing oxygen whose purity has to be kept permanently at least at 90% by volume, which constitutes the desired purity threshold value (VPS). - The oxygen produced is recovered at the output of the O2 VSA (zone 1) and conveyed to a container (not shown) as far as a client site (zone 4) by means of at least one compressor (zone 2) by means of a pipeline.
- In order to control the oxygen flow rate, the recirculation valve Qr is driven according to a flow rate control loop or “
loop FIC 1”. The function of the latter is to limit the production flow rate (Dp) of the unit to the value set by the operator, irrespective of the client demand (Du). - The regulation principle of the invention therefore consists in adapting the reference of the
loop FIC 1 as a function of the oxygen purity measurement (Pp). - In other words, the principle of the control loop consists in adapting the production flow rate limit (Dp) in real time in order to ensure a purity at the capacity limits of the VSA unit. This adaptation is obtained by virtue of the functional diagram given in
FIG. 3 and employing a so-called “predictive” or “Smith predictor” regulation algorithm. - The advantage of this type of regulation is that it “predicts” the O2 purity (Pp) by virtue of a model giving a modeled purity (Ppm), and thus allowing regulation by anticipation.
- Installing this regulation system then makes it possible to have a distribution of the purity around the VPS with a standard deviation difference less than 0.5%, typically of the order of 0.1%, as shown by the curves of
FIG. 4 , independently of the day/night cycles. - However, as illustrated in
FIG. 2 , when the user flow rate (Du) becomes greater than the production flow rate (Dp), this oxygen demand is compensated for by introducing backup oxygen coming from a source of liquid oxygen (LOX), which is connected to the pipeline carrying the gaseous oxygen from the VSA to the user site. The LOX is vaporized beforehand prior to its injection into the pipeline (zone 3). A working oxygen purity value (Pu) is thus obtained such that VPS=Pu+X where Pu is the O2 purity measured downstream of the site of introduction of the LOX into the pipeline. - This injection of backup LOX is particularly advantageous because it makes it possible to cater for peaks in oxygen demand from the user site.
Claims (10)
1-9. (canceled)
10. A method for producing gaseous oxygen from compressed air by adsorption, the method comprising the steps of:
a) producing a gaseous oxygen by flowing the compressed air through at least one adsorption unit with a variable production flow rate (Dp), measuring a first purity of the gaseous oxygen and verifying a purity greater than or equal to a predetermined purity threshold value (VPS)
b) recovering the gaseous oxygen produced in step a) and conveying the gaseous oxygen through at least one gas pipeline to a user site or storage site,
c) measuring a second purity of the gaseous oxygen (Pp) produced in step a) and carried by said gas pipeline before the gaseous oxygen reaches the user site or storage site and comparing the second purity with the predetermined purity threshold value (VPS),
d) adjusting an oxygen production flow rate (Dp) before the user site or storage site as a function of the comparison carried out in step c) so that:
i) the oxygen production flow rate (Dp) is reduced when the oxygen purity (Pp) measured in step c) is such that: VPS>Pp or
ii) the production flow rate (Dp) is increased when the oxygen purity (Pp) determined in step c) is such that: VPS<Pp
so as to obtain a gaseous oxygen purity (Pp) such that:
VPS=Pp+X with X being the standard deviation and X<0.5%.
VPS=Pp+X with X being the standard deviation and X<0.5%.
e) sending the produced oxygen at a production flow rate (Dp) to a user site, and
f) adding oxygen coming from a source of liquid oxygen (LOX) to the gas pipeline when a rate of oxygen consumed by the user site (Du) is such that Du>Dp, the liquid oxygen being vaporized before its introduction into the gas pipeline, so as to obtain a given user oxygen purity (Pu) such that: VPS=Pu+X
where:
the oxygen purity (Pu) is measured on the pipeline downstream of the injection site of liquid oxygen (LOX).
11. The method as claimed in claim 10 , wherein the oxygen production flow rate is adjusted in step d) so that VPS=Pp+X with X<0.3%.
12. The method of claim 10 , wherein the oxygen production flow rate is adjusted in step d) so that VPS=Pp+X with X<0.1%.
13. The method of claim 10 wherein the recovered gaseous oxygen is compressed in step b) before it is conveyed to the user site by means of the gas pipeline.
14. The method of claim 10 , wherein the gaseous oxygen is produced in step a) by a VSA or PSA adsorption unit.
15. The method of claim 10 wherein that the purity threshold value (VPS) is at least 70% by volume.
16. The method of claim 10 wherein the oxygen is produced in step a) by separation of air by adsorption of nitrogen on at least one adsorbent which adsorbs nitrogen preferentially to oxygen.
17. The method of claim 10 wherein the oxygen production flow rate is adjusted in step d) by acting on an opening of a recirculation valve situated on a bypass line formed on the gas pipeline carrying the produced oxygen, said bypass line configured to bypass at least one gas compressor situated on said gas pipeline, downstream of the adsorption unit, and furthermore serving to recycle, upstream of said at least one compressor, oxygen collected downstream of said compressor.
18. The method of claim 10 wherein
the production flow rate (Dp) is between 100 and 6000 Nm3/h;
the user flow rate (Du) is between 100 and 10 000 Nm3/h;
the purity (Pp) of the oxygen is between 88 and 95%; and
the user oxygen purity (Pu) is between 88 and 100%.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0953965A FR2946546B1 (en) | 2009-06-15 | 2009-06-15 | PROCESS FOR REGULATING THE OXYGEN PURITY PRODUCED BY A FLOW CONTROL ADSORPTION UNIT |
FR0953965 | 2009-06-15 | ||
PCT/FR2010/051116 WO2010146282A1 (en) | 2009-06-15 | 2010-06-07 | Method for adjusting the purity of oxygen generated by an adsorption unit by controlling the flow rate |
Publications (1)
Publication Number | Publication Date |
---|---|
US20120103186A1 true US20120103186A1 (en) | 2012-05-03 |
Family
ID=41581008
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US13/378,062 Abandoned US20120103186A1 (en) | 2009-06-15 | 2010-06-07 | Method For Adjusting The Purity Of Oxygen Generated By An Adsorption Unit By Controlling The Flow Rate |
Country Status (9)
Country | Link |
---|---|
US (1) | US20120103186A1 (en) |
EP (1) | EP2442890A1 (en) |
JP (1) | JP2012530038A (en) |
CN (1) | CN102802765A (en) |
BR (1) | BRPI1011370A2 (en) |
CA (1) | CA2761188A1 (en) |
FR (1) | FR2946546B1 (en) |
RU (1) | RU2534086C2 (en) |
WO (1) | WO2010146282A1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10821453B2 (en) | 2016-10-07 | 2020-11-03 | Hansgrohe Se | Shower jet generating device |
US11491498B2 (en) | 2016-12-22 | 2022-11-08 | Hansgrohe Se | Shower jet outlet device and shower device equipped therewith |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9023245B2 (en) * | 2013-04-26 | 2015-05-05 | Praxair Technology, Inc. | Method and system for producing a synthesis gas using an oxygen transport membrane based reforming system with secondary reforming |
FR3011481B1 (en) * | 2013-10-04 | 2017-01-20 | Air Liquide | PRESSURE MODULATION ADSORPTION METHOD WITH REGULATION |
BE1023373B1 (en) * | 2015-06-12 | 2017-02-24 | Atlas Copco Airpower,Naamloze Vennootschap | Method for controlling an adsorption phase of a gas generator and a gas generator applying such a method. |
US10415760B2 (en) * | 2017-04-18 | 2019-09-17 | Air Products And Chemicals, Inc. | Control system in an industrial gas pipeline network to satisfy energy consumption constraints at production plants |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5917135A (en) * | 1996-06-14 | 1999-06-29 | Invacare Corporation | Gas concentration sensor and control for oxygen concentrator utilizing gas concentration sensor |
US7329304B2 (en) * | 2005-04-05 | 2008-02-12 | Respironics Oxytec, Inc. | Portable oxygen concentrator |
WO2009063938A1 (en) * | 2007-11-15 | 2009-05-22 | Teijin Pharma Limited | Oxygen concentrator |
US7601202B2 (en) * | 2003-01-07 | 2009-10-13 | Blue Membranes Gmbh | Method and device for reducing the carbon dioxide concentration in air |
US20110232482A1 (en) * | 2010-03-29 | 2011-09-29 | Wearair Oxygen, Inc. | Moisture Mitigation in PSA Air Fractionation |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2837281A1 (en) * | 1978-08-25 | 1980-03-06 | Linde Ag | Respirable gas supply for aircraft cabins - by adsorptive removal of nitrogen from compressed air |
US4725293A (en) * | 1986-11-03 | 1988-02-16 | The Boc Group, Inc. | Automatic control for Pressure Swing Adsorption system |
US4867766A (en) * | 1988-09-12 | 1989-09-19 | Union Carbide Corporation | Oxygen enriched air system |
US5258056A (en) * | 1991-09-27 | 1993-11-02 | The Boc Group, Inc. | PSA system with product turndown and purity control |
RU2158610C2 (en) * | 1998-12-15 | 2000-11-10 | Научно-техническое объединение "Био-Нова" | Method and apparatus for regulating and controlling of oxygen concentration |
-
2009
- 2009-06-15 FR FR0953965A patent/FR2946546B1/en not_active Expired - Fee Related
-
2010
- 2010-06-07 EP EP10734508A patent/EP2442890A1/en not_active Withdrawn
- 2010-06-07 BR BRPI1011370A patent/BRPI1011370A2/en not_active Application Discontinuation
- 2010-06-07 WO PCT/FR2010/051116 patent/WO2010146282A1/en active Application Filing
- 2010-06-07 CN CN2010800265619A patent/CN102802765A/en active Pending
- 2010-06-07 US US13/378,062 patent/US20120103186A1/en not_active Abandoned
- 2010-06-07 CA CA2761188A patent/CA2761188A1/en not_active Abandoned
- 2010-06-07 JP JP2012515541A patent/JP2012530038A/en not_active Withdrawn
- 2010-06-07 RU RU2012101271/05A patent/RU2534086C2/en not_active IP Right Cessation
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5917135A (en) * | 1996-06-14 | 1999-06-29 | Invacare Corporation | Gas concentration sensor and control for oxygen concentrator utilizing gas concentration sensor |
US7601202B2 (en) * | 2003-01-07 | 2009-10-13 | Blue Membranes Gmbh | Method and device for reducing the carbon dioxide concentration in air |
US7329304B2 (en) * | 2005-04-05 | 2008-02-12 | Respironics Oxytec, Inc. | Portable oxygen concentrator |
WO2009063938A1 (en) * | 2007-11-15 | 2009-05-22 | Teijin Pharma Limited | Oxygen concentrator |
US20100242734A1 (en) * | 2007-11-15 | 2010-09-30 | Teijin Pharma Limited | Oxygen concentrator |
US20110232482A1 (en) * | 2010-03-29 | 2011-09-29 | Wearair Oxygen, Inc. | Moisture Mitigation in PSA Air Fractionation |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10821453B2 (en) | 2016-10-07 | 2020-11-03 | Hansgrohe Se | Shower jet generating device |
US11491498B2 (en) | 2016-12-22 | 2022-11-08 | Hansgrohe Se | Shower jet outlet device and shower device equipped therewith |
Also Published As
Publication number | Publication date |
---|---|
EP2442890A1 (en) | 2012-04-25 |
WO2010146282A1 (en) | 2010-12-23 |
CN102802765A (en) | 2012-11-28 |
CA2761188A1 (en) | 2010-12-23 |
FR2946546B1 (en) | 2012-06-08 |
FR2946546A1 (en) | 2010-12-17 |
JP2012530038A (en) | 2012-11-29 |
RU2534086C2 (en) | 2014-11-27 |
BRPI1011370A2 (en) | 2016-03-15 |
RU2012101271A (en) | 2013-07-27 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20120103186A1 (en) | Method For Adjusting The Purity Of Oxygen Generated By An Adsorption Unit By Controlling The Flow Rate | |
EP0932439B1 (en) | Closed-loop feedback control for oxygen concentrator | |
US5258056A (en) | PSA system with product turndown and purity control | |
KR101458395B1 (en) | Oxygen concentrator | |
US7789939B2 (en) | Adsorbent bed repressurization control method | |
US20120272966A1 (en) | Oxygen enrichment device | |
KR20010070418A (en) | Low pressure ratio vpsa plant tuning and balancing system | |
EP3421070B1 (en) | Oxygen concentrator | |
AU2017245115A2 (en) | Pressure swing adsorption type gas manufacturing device | |
JP5758745B2 (en) | Gas supply system and gas supply method | |
CN211274123U (en) | Oxygen-enriched tail gas recovery device of pressure swing adsorption nitrogen making machine | |
KR101969614B1 (en) | Product gas supply method and product gas supply system | |
JPS63307101A (en) | Pressure swing adsorption type production of oxygen | |
JP5864994B2 (en) | Gas separation apparatus and method | |
JP5013855B2 (en) | Gas production method and gas production apparatus using gas separation membrane | |
JP2022029786A (en) | Air separation device and production method of oxygen and/or nitrogen | |
JP7446569B2 (en) | Product gas supply amount adjustment device and air separation device equipped with the same | |
KR101498269B1 (en) | Nitrogen generator | |
CN219244069U (en) | Gas preparation is with advancing pressure compensating system | |
KR100372032B1 (en) | An apparatus for controlling the oxygen purity | |
JPH08173744A (en) | Method for controlling supply amount of product gas in pressure variation adsorption separator | |
JP3300898B2 (en) | Nitrogen production apparatus and its operation method | |
CN114768470A (en) | Pressure swing adsorption gas separation equipment and method, and regulation metering control system and method | |
CN116651144A (en) | Control method of energy-saving pressure swing adsorption gas making equipment | |
JP2011226383A (en) | Oxygen concentrator |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: L'AIR LIQUIDE SOCIETE ANONYME POUR L'ETUDE ET L'EX Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:PIERQUIN, JOSEPH;FOURAGE, SYLVAIN;ROY, OLIVIER;SIGNING DATES FROM 20110909 TO 20110917;REEL/FRAME:027384/0869 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO PAY ISSUE FEE |